US4094814A - Regeneration method for gravity-flowing deactivated catalyst particles - Google Patents

Regeneration method for gravity-flowing deactivated catalyst particles Download PDF

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US4094814A
US4094814A US05/806,885 US80688577A US4094814A US 4094814 A US4094814 A US 4094814A US 80688577 A US80688577 A US 80688577A US 4094814 A US4094814 A US 4094814A
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section
burning
catalyst particles
halogen
carbon
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US05/806,885
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Earl S. Lemberger
Robert K. Olson
Lester F. Smith
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Honeywell UOP LLC
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UOP LLC
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Priority to US05/806,885 priority Critical patent/US4094814A/en
Priority to SE7806774A priority patent/SE436694B/sv
Priority to JP7068678A priority patent/JPS545894A/ja
Priority to ES470706A priority patent/ES470706A1/es
Priority to GB7826798A priority patent/GB2000044B/en
Priority to DE19782825811 priority patent/DE2825811A1/de
Priority to NL7806382A priority patent/NL7806382A/xx
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Publication of US4094814A publication Critical patent/US4094814A/en
Priority to PT68166A priority patent/PT68166A/pt
Priority to FR7817830A priority patent/FR2394323A1/fr
Assigned to UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP reassignment UOP, DES PLAINES, IL, A NY GENERAL PARTNERSHIP ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: KATALISTIKS INTERNATIONAL, INC., A CORP. OF MD
Assigned to UOP, A GENERAL PARTNERSHIP OF NY reassignment UOP, A GENERAL PARTNERSHIP OF NY ASSIGNMENT OF ASSIGNORS INTEREST. Assignors: UOP INC.
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    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J8/00—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes
    • B01J8/08—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles
    • B01J8/12—Chemical or physical processes in general, conducted in the presence of fluids and solid particles; Apparatus for such processes with moving particles moved by gravity in a downward flow
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/90—Regeneration or reactivation
    • B01J23/94—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the iron group metals or copper
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J23/00—Catalysts comprising metals or metal oxides or hydroxides, not provided for in group B01J21/00
    • B01J23/90—Regeneration or reactivation
    • B01J23/96—Regeneration or reactivation of catalysts comprising metals, oxides or hydroxides of the noble metals
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01J—CHEMICAL OR PHYSICAL PROCESSES, e.g. CATALYSIS OR COLLOID CHEMISTRY; THEIR RELEVANT APPARATUS
    • B01J37/00—Processes, in general, for preparing catalysts; Processes, in general, for activation of catalysts
    • B01J37/22—Halogenating
    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G35/00—Reforming naphtha
    • C10G35/04—Catalytic reforming
    • C10G35/10—Catalytic reforming with moving catalysts
    • C10G35/12—Catalytic reforming with moving catalysts according to the "moving-bed" method

Definitions

  • Movable beds of particulate solids are currently employed in, or are applicable to a wide variety of systems. It is to such systems -- i.e. those containing a bed of solids movable therethrough via gravity-flow -- that the inventive concept of the present invention is applicable. More specifically, our invention is directed toward a system for the catalytic conversion of hydrocarbonaceous material, in which system deactivated catalyst particles are regenerated in a zone, or chamber through which the particles are downwardly movable via gravityflow.
  • the catalytic reforming process utilized a catalytic composite of a Group VIII noble metal component and a halogen component combined with a refractory inorganic oxide, and was effected in a non-regenerative, fixed-bed system consisting of a plurality of reaction zones in side-by-side relation.
  • a catalytic composite became deactivated to the extent that continued operation was no longer economically feasible, the entire unit was shut down, and the catalyst regenerated in situ. After several such regenerations, the catalyst was replaced with fresh catalyst and the deactivated catalyst subjected either to an exotic reconditioning technique, or an involved method for the recovery of the precious noble metal.
  • the so-called "swing-bed" system in which an extra reactor was substituted for one due to be placed off-stream for regeneration purposes.
  • a "stacked" reactor system in which the catalyst particles flow, via gravity, downwardly from one annular-form catalyst zone to another.
  • the catalyst is transferred to a suitable regeneration system also functioning with a downwardly-moving bed of catalyst.
  • the catalyst particles are maintained within the reaction system, and continuously transferred from one section to another in a manner such that the flow is continuous, at frequent intervals, or at extended intervals, the movement thereof being controlled by the quantity of catalyst withdrawn from the last in the series of individual reaction zones.
  • a principal object of our invention is to provide an improved method for continuously regenerating deactivated hydrocarbon conversion catalyst particles.
  • a corollary objective involves a method for regenerating deactivated catalyst particles, comprising a Group VIII noble metal component and a halogen component in conbination with a refractory inorganic oxide, in a regeneration zone through which said catalyst particles are movable via gravity-flow.
  • Another object of our invention is to afford to more economical technique for regenerating catalyst particles which have been deactivated by deposition of carbonaceous matter thereon and loss of halogen therefrom.
  • our invention is directed toward a method for continuously regenerating hydrocarbon conversion catalyst particles comprising a Group VIII metal component and a halogen component in combination with a refractory inorganic oxide carrier material, and which have become deactivated (1) by deposition of carbonaceous matter thereon and, (2) through loss of halogen therefrom, in a regeneration zone through which said catalyst particles are downwardly movable via gravity-flow, which regeneration method comprises the inter-related steps of: (a) introducing (i) deactivated catalyst particles, (ii) a first air stream from an external source and, (iii) a first mixture of steam and a halogen, or halogen-containing compound, into a first carbon-burning/ halogenation section; (b) maintaining said catalyst particles within said first section for a time sufficient to (i) remove the greater portion of said carbonaceous matter therefrom and, (ii) increase the halogen content thereof; (c) introducing (i) the catalyst particles from said first section, via gravity-flow, (
  • the temperature in the first and second carbon-burning/halogenation sections is maintained in the range of about 750° to about 1050° F.
  • the temperature in the lower drying section will be from about 830° to about 1000° F.
  • the excess air and the combustion products resulting from the burning of carbon are withdrawn from the carbon-burning/halogenation zone, cooled and at least in part recycled to both the first and second carbon-burning sections.
  • U.S. Pat. No. 3,470,090 illustrates a side-by-side reaction system having intermediate heating of the reactant stream. Catalyst withdrawn from an individual reaction zone is transported to suitable regeneration facilities. This particular type of system can be modified such that the catalyst withdrawn from a given reaction zone is sent to the next succeeding reaction zone, while that catalyst withdrawn from the last reaction zone is transported to regeneration facilities. This latter technique is illustrated by U.S. Pat. Nos. 3,647,680 and 3,785,963.
  • the catalytic reforming configuration is shown as a two-stage "stacked" system having an integrated regeneration facility which receives the catalyst particles withdrawn from the bottom reaction chamber. As illustrated, both techniques utilize a downwardly-moving bed of catalyst particles through the stacked reaction zones and through the regeneration chamber.
  • U.S. Pat. No. 3,652,231 describes a reconditioning, or regeneration system for a moving column of reforming catalyst. It is to this type of regeneration system that our invention is particularly directed, and affords a distinct improvement therein.
  • a regeneration technique for gravity-flowing catalyst particles is disclosed in U.S. Pat. No. 3,981,824, issued Sept. 21, 1976.
  • Three distinct zones for complete regeneration are employed: (1) a carbon-burning zone, into which the catalyst particles are initially introduced; (2) a halogenation zone; and, (3) a lowermost catalyst-drying zone.
  • Flue gas vapors from the carbon-burning section are at least in part recycled thereto.
  • vapors from the drying and halogenation sections are recycled to the halogenation section.
  • at least a portion of the effluent vapors from the halogenation section are caused to bypass the recycle conduit and enter the carbon-burning section.
  • a portion of substantially dry air is introduced into a heater and therefrom into the lower drying section.
  • a second portion of the air stream is combined with the recycled flue gas for introduction therewith into the carbon-burning section.
  • Steam and halogen, in admixture with effluent vapors from the drying and halogenation sections, are introduced into a second heater and therefrom into the halogenation section.
  • the main thrust of this described technique involves three-zone regeneration accompanied by split air flow to the drying and carbon-burning sections.
  • the technique encompassed by our inventive concept differs from the foregoing three-zone regeneration method in several important aspects which lead to significant advantages and/or benefits.
  • Initially there exists a simplification of the regeneration tower design relative to the internal hardware. Total residence time of the catalyst particles, within the regeneration tower is reduced; thus, changes in regeneration are more quickly observed at the various sample points and especially in the reactor section itself. Start-up procedures become much more simplified; the time required for the start-up procedure is reduced from about 24 hours to about 16 hours, and this greatly lessens the risk of catalyst damage. Simultaneous carbon-burning and halogenation reduces the likelihood of noble metal agglomeration; thus, the metallic components retain their active, dispersed state.
  • the second section serves as a quasi halogen-adjustment section, while simultaneously removing the remaining carbonaceous material. Also, the length of the time required for catalyst regeneration/reconditioning is lessened by approximately one-third; this will afford an increase in total spent catalyst throughput, for a given size regeneration tower, or a corresponding increase in coke-burning capacity.
  • our invention is intended to effect the regeneration of deactivated hydrocarbon conversion catalyst particles comprising a Group VIII noble metal component and halogen component combined with a refractory inorganic oxide.
  • Group VIII noble metal component is intended to include ruthenium, rhodium, palladium, osmium, iridium, platinum, and mixtures thereof.
  • our regeneration method is applicable to the recently-developed bi-, tri- and tetra-metallic catalysts in which metallic components other than those of the Group VIII noble metals are incorporated therewith.
  • Such other metallic components include technetium, rhenium, gallium, vanadium, cobalt, nickel, gold, germanium, tin, lead, bismuth, etc.
  • the quantity of the Group VIII noble metal components within the final catalytic composite is small compared to the quantities of the other components combined therewith, and will be present in an amount of about 0.01% to about 2.0% by weight of the final catalytic composite, calculated on an elemental basis.
  • the other metallic components, hereinabove set forth will be present in an amount in the range of about 0.01% to about 5.0%, again calculated on an elemental basis.
  • halogen component Another ingredient of the type of catalytic composites regenerated by the present method is a halogen component.
  • halogen component may be either fluorine, chlorine, iodine, bromine, or mixtures thereof, with fluorine and particularly chlorine being preferred.
  • the halogen component will be present within the catalyst in an amount within the range of about 0.1% to about 5.0%, and generally from about 0.5% to about 1.5% by weight, calculated on an elemental basis.
  • One or more of the foregoing metallic components and the halogen component is combined with a suitable refractory inorganic oxide carrier material.
  • compositions including alumina, silica, zirconia, hafnia, boria, thoria, mixtures thereof, etc.; however, with respect to the catalytic reforming of hydrocarbons, alumina in and of itself, is generally preferred.
  • the regeneration zone is shown as having an upper carbon-burning section, an intermediate halogenation section and a lower drying section.
  • Catalyst particles are introduced initially into the top of the regeneration zone, pass downwardly through the carbon-burning section into the halogenation section and finally into the lower drying section. All the air required for reconditioning is introduced into the lower drying section and passes upwardly therefrom into the halogenation section, and therethrough into the carbon-burning section.
  • Halogen and steam are introduced into the intermediate halogenation section, and any excess is recycled in admixture with fresh steam and halogen.
  • combustion vapors from the carbon-burning section are introduced into a caustic scrubbing facility, and thereafter recycled to the carbon-burning section.
  • Another three-stage regeneration technique is that set forth in the previously described U.S. Pat. No. 3,981,824; however, the aspect of split air flow is incorporated therein.
  • Our catalyst regeneration technique is intended to improve significantly both of the above-described techniques. To reiterate briefly, the regeneration technique is accomplished in two discreet zones, as contrasted to the three zones of the prior art.
  • substantially dry air is introduced to the lower drying zone and undried air to the upper carbon-burning/halogenation zone. With respect to the latter, the air is admixed with the steam/halogen mixture and recycled flue gas, and introduced therewith into this dual-function zone.
  • the combined carbon-burning/halogenation zone is divided into two sections, into both of which the mixture of flue gas, steam, halogen and air is introduced.
  • the mole ratio of air introduced into both carbon-burning sections, to that introduced into the drying zone is at least 1.0:1.0, and generally in the range of about 1.0:1.0 to about 9.0:1.0.
  • the quantity (or proportion) of air introduced into the drying zones will be the minimum sufficient to accomplish the necessary drying.
  • the flue gas from the carbon-burning/halogenation sections is recycled thereto without any intermediate treatment, excepting the cooling thereof.
  • the relative rates of the dry air and flue gas recycle are maintained to control the oxygen concentration at a level in the range of about 0.2% to 2.0%, on a model basis, and preferably from about 0.5% to about 1.5%.
  • the upper section of the regeneration tower essentially serves two principal functions; first, the coke and/or carbonaceous material must be removed from the catalyst particles and, secondly, the halogen content must be increased while simultaneously properly dispersing the metallic components.
  • split air flow i.e. introducing from about 10.0% to about 50.0% of the required air into the lower drying zone -- is to maintain the necessary partial pressure of halogen in the upper combined carbon-burning/halogenation zone with less overall fresh halogen addition.
  • combining the halogenation and carbon-burning functions alleviates noble metal agglomeration normally occurring when the carbonaceous material is removed from the catalyst particles.
  • the concentration will be about 1.1% by weight following halogenation and carbon burning, and about 1.0% by weight following the drying step.
  • a regenerating tower 1 having an upper, first carbon-burning/halogenation section 2, a lower, second carbon-burning/halogenation section 3 and a lower drying zone 4.
  • Catalyst particles which have been withdrawn from the lower terminus of a reaction zone, through which they are movable via gravity-flow, are transported to regenerating tower 1 by way of lift line 9 and are introduced thereby into disengaging hopper 10. Catalyst particles are disengaged from dustlike catalyst fines which are removed from the regeneration facility by way of conduit 11, and transported thereby to a dust collector.
  • Separated catalyst particles flow downwardly through a plurality of inlet conduits 12, generally numbering from about four to 16, and into annular-form space 8.
  • the latter is formed by a perforated centerpipe 7 and an outer catalyst-retaining screen 6, through which the reconditioning vapors pass.
  • the catalyst particles at a temperature of about 210° F., initially traverse carbon-burning/halogenation section 2 which functions in the temperature range of about 830° F. (443° C.) to about 990° F. (532° C.).
  • Catalyst-burning/halogenation section 2 is that portion of the regenerating tower which extends from the top plate to a horizontally-disposed baffle 5.
  • the second carbon-burning/halogenation section 3 also functioning at about 830° F. (443° C.) to about 990° F. (532° C.), is that portion of regeneration tower 1 below horizontal baffle 5 and the terminal end of perforated centerpipe 7.
  • Substantially carbon-free catalyst particles flow via gravity into lower drying zone 4 which is maintained at an elevated temperature of about 830° F. (443° C.) to about 1000° F. (538° C.); that is, substantially dry air, introduced into the frusto-conical section by way of line 25, is at a temperature of about 1000° F. (538° C.), while catalyst particles emanating from the regenerating tower, via outlet port 13 and line 14, are at a temperature of about 830° F. (443° C.). Dried, reconditioned catalyst particles are subjected to hydrogen reduction either in a separate vessel prior to being transported to the reaction zone, or in a vessel which is an integral part of the reaction zone.
  • At least a portion of the effluent vapors, flue gas, emanating from the carbon-burning/halogenation sections of the regeneration tower 1, are recycled thereto.
  • the oxygen concentration within this upper zone is regulated and maintained in the preferred range of about 0.5% to about 1.5%.
  • dilution of the halogen-steam atmosphere within the carbon-burning/halogenation sections is effected by the vapors emanating from the drying section. This relatively severe oxidizing atmosphere facilitates the redistribution of the noble metal component.
  • a mixture of steam and halogen, or a halogen-containing compound is introduced by way of line 26, admixed with recycled flue gas from line 18, and the remaining portion of substantially air from line 20. Approximately 1/2 to 2/3 of the resulting mixture is diverted through line 27 and blower 28 into conduit 29, through which it is introduced into upper carbon-burning/halogenation section 2.
  • This halogen-containing stream is at a temperature of about 830° F. (443° C.).
  • the halogen for example chlorine, may be employed in its elemental state, or as a compound such as hydrogen chloride, ethylene dichloride, propylene dichloride, tertiary butyl chloride, etc.
  • halogen addition takes the form of a steam/hydrogen chloride mixture entering by way of conduit 26; of the 0.44 moles/hr., about 0.13 moles is hydrogen chloride.
  • Effluent vapors from upper carbon-burning/halogenation section 2 at a temperature of about 930° F. (498° C.), are withdrawn through the extension of centerpipe 7 and outlet port 15; these are introduced, by way of line 16, into cooler 17, wherein the temperature is decreased to about 840° F. (449° C.).
  • cooled vapors are withdrawn via line 18, and about 400 moles/hr. continue therethrough.
  • the remaining portion of the cooled flue gas vapors are vented from the system through conduit 19.
  • the catalyst particles introduced into the regeneration zone from disengaging hopper 10, contain about 26.1 lbs/hr. (11.8 kg/hr.) of coke and about 0.75% by weight of combined chloride.
  • These leave the carbon-burning/halogenation sections they are substantially coke-free; the halogen content has been increased to about 1.1% by weight, and the catalyst particles contain about 0.90% by weight of water.
  • the latter is removed in the drying zone, and the dried catalyst particles are withdrawn from the regeneration zone containing 1.0% by weight of halogen.
  • the upper carbon-burning/halogenation sections and the lower drying zone, of the regeneration zone 1, are sized and designed to provide an effective residence time, of the catalyst particles passing through each section, of from 1 to about 3 hours.

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  • Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
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  • Materials Engineering (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Catalysts (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
US05/806,885 1977-06-15 1977-06-15 Regeneration method for gravity-flowing deactivated catalyst particles Expired - Lifetime US4094814A (en)

Priority Applications (9)

Application Number Priority Date Filing Date Title
US05/806,885 US4094814A (en) 1977-06-15 1977-06-15 Regeneration method for gravity-flowing deactivated catalyst particles
JP7068678A JPS545894A (en) 1977-06-15 1978-06-12 Method of continuously regenerating hydrocarbon conversion catalyst particle
ES470706A ES470706A1 (es) 1977-06-15 1978-06-12 Un metodo para regenerar continuamente particulas de catali-zador de conversion de hidrocarburos
SE7806774A SE436694B (sv) 1977-06-15 1978-06-12 Kontinuerligt forfarande for regenerering av deaktiverade katalysatorer, samtidig kolforbrenning och halogenering
DE19782825811 DE2825811A1 (de) 1977-06-15 1978-06-13 Verfahren zum kontinuierlichen regenerieren von teilchenfoermigen kohlenwasserstoffumwandlungskatalysatoren
NL7806382A NL7806382A (nl) 1977-06-15 1978-06-13 Werkwijze voor het continu regenereren van koolwater- stof-conversiekatalysatoren.
GB7826798A GB2000044B (en) 1977-06-15 1978-06-13 Regeneration method for gravity-flowing deactivated catalyst particles
PT68166A PT68166A (en) 1977-06-15 1978-06-14 Regeneration method for gravity-flowing deactivated catalyst-particles
FR7817830A FR2394323A1 (fr) 1977-06-15 1978-06-14 Procede de regeneration de particules d'un catalyseur desactive s'ecoulant par gravite

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US05/806,885 US4094814A (en) 1977-06-15 1977-06-15 Regeneration method for gravity-flowing deactivated catalyst particles

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US (1) US4094814A (es)
JP (1) JPS545894A (es)
DE (1) DE2825811A1 (es)
ES (1) ES470706A1 (es)
FR (1) FR2394323A1 (es)
GB (1) GB2000044B (es)
NL (1) NL7806382A (es)
PT (1) PT68166A (es)
SE (1) SE436694B (es)

Cited By (11)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US4578370A (en) * 1985-04-25 1986-03-25 Uop Inc. Gas circulation method for moving bed catalyst regeneration zones
US4647549A (en) * 1985-12-27 1987-03-03 Upo Inc. Regeneration of hydrocarbon conversion catalyst
US4701429A (en) * 1986-02-03 1987-10-20 Uop Inc. Catalyst regeneration with varying air flow to burn-off zone from drying zone through halogenation zone
FR2611533A1 (fr) * 1987-02-26 1988-09-09 Inst Francais Du Petrole Procede de regeneration de catalyseurs de conversion d'hydrocarbures, a base de zeolithe
EP0283603A1 (en) * 1987-02-24 1988-09-28 Mobil Oil Corporation Redispersion of agglomerated noble metals on zeolite catalysts
US4810683A (en) * 1988-01-25 1989-03-07 Uop Inc. Regeneration of a platinum-containing zeolite
US4867950A (en) * 1987-10-13 1989-09-19 Mobil Oil Corporation Catalyst regeneration with flue gas
US8716161B2 (en) 2012-03-05 2014-05-06 Chevron Phillips Chemical Company Methods of regenerating aromatization catalysts
US8912108B2 (en) 2012-03-05 2014-12-16 Chevron Phillips Chemical Company Lp Methods of regenerating aromatization catalysts
US9387467B2 (en) 2012-09-26 2016-07-12 Chevron Phillips Chemical Company Lp Aromatization catalysts with high surface area and pore volume
US10240097B2 (en) 2015-03-31 2019-03-26 Uop Llc Methods and apparatuses for an integrated isomerization and platforming process

Families Citing this family (1)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
DE19621943C2 (de) * 1996-05-31 2000-12-07 Daimler Chrysler Ag Stirnwand für eine Fahrzeugkarosserie

Citations (3)

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Publication number Priority date Publication date Assignee Title
US3652231A (en) * 1969-09-25 1972-03-28 Universal Oil Prod Co Reconditioning system for moving column of reforming catalyst
US3725249A (en) * 1971-12-14 1973-04-03 Universal Oil Prod Co Continuous reforming-regeneration process
DE2548130A1 (de) * 1974-11-13 1976-05-20 Uop Inc Regenerierverfahren fuer katalysatorteilchen unter schwerkraftfluss

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Publication number Priority date Publication date Assignee Title
FR1298761A (fr) * 1960-08-29 1962-07-13 Universal Oil Prod Co Procédé pour activer un catalyseur contenant un métal noble

Patent Citations (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3652231A (en) * 1969-09-25 1972-03-28 Universal Oil Prod Co Reconditioning system for moving column of reforming catalyst
US3725249A (en) * 1971-12-14 1973-04-03 Universal Oil Prod Co Continuous reforming-regeneration process
DE2548130A1 (de) * 1974-11-13 1976-05-20 Uop Inc Regenerierverfahren fuer katalysatorteilchen unter schwerkraftfluss

Cited By (18)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
EP0200474A1 (en) * 1985-04-25 1986-11-05 Uop Process for regenerating coke-contaminated catalyst
AU574916B2 (en) * 1985-04-25 1988-07-14 Uop Inc. Regeneration of coke contaminated catalyst
US4578370A (en) * 1985-04-25 1986-03-25 Uop Inc. Gas circulation method for moving bed catalyst regeneration zones
US4647549A (en) * 1985-12-27 1987-03-03 Upo Inc. Regeneration of hydrocarbon conversion catalyst
AU581113B2 (en) * 1985-12-27 1989-02-09 Uop Inc. Method and apparatus for regeneration of hydrocarbon conversion catalyst
US4701429A (en) * 1986-02-03 1987-10-20 Uop Inc. Catalyst regeneration with varying air flow to burn-off zone from drying zone through halogenation zone
EP0283603A1 (en) * 1987-02-24 1988-09-28 Mobil Oil Corporation Redispersion of agglomerated noble metals on zeolite catalysts
FR2611533A1 (fr) * 1987-02-26 1988-09-09 Inst Francais Du Petrole Procede de regeneration de catalyseurs de conversion d'hydrocarbures, a base de zeolithe
US4867950A (en) * 1987-10-13 1989-09-19 Mobil Oil Corporation Catalyst regeneration with flue gas
US4810683A (en) * 1988-01-25 1989-03-07 Uop Inc. Regeneration of a platinum-containing zeolite
US8716161B2 (en) 2012-03-05 2014-05-06 Chevron Phillips Chemical Company Methods of regenerating aromatization catalysts
US8912108B2 (en) 2012-03-05 2014-12-16 Chevron Phillips Chemical Company Lp Methods of regenerating aromatization catalysts
US9174895B2 (en) 2012-03-05 2015-11-03 Chevron Phillips Chemical Company Lp Methods of regenerating aromatization catalysts
US9421530B2 (en) 2012-03-05 2016-08-23 Chevron Phillips Chemical Company Lp Methods of regenerating aromatization catalysts
US9943837B2 (en) 2012-03-05 2018-04-17 Chevron Phillips Chemical Company Lp Methods of regenerating aromatization catalysts
US9387467B2 (en) 2012-09-26 2016-07-12 Chevron Phillips Chemical Company Lp Aromatization catalysts with high surface area and pore volume
US10183284B2 (en) 2012-09-26 2019-01-22 Chevron Phillips Chemical Company Lp Aromatization catalysts with high surface area and pore volume
US10240097B2 (en) 2015-03-31 2019-03-26 Uop Llc Methods and apparatuses for an integrated isomerization and platforming process

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ES470706A1 (es) 1979-01-16
DE2825811A1 (de) 1979-01-04
SE436694B (sv) 1985-01-21
SE7806774L (sv) 1978-12-16
JPS545894A (en) 1979-01-17
NL7806382A (nl) 1978-12-19
FR2394323A1 (fr) 1979-01-12
PT68166A (en) 1978-07-01
GB2000044A (en) 1979-01-04
DE2825811C2 (es) 1988-10-27
FR2394323B1 (es) 1983-02-11
GB2000044B (en) 1982-01-27

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